Particulate polyamide, and method for preparing the particulate polyamide

ABSTRACT

A particulate polyamide is provided. The particulate polyamide is porous and includes at least one of polyamide 4 and polyamide 3. In addition, the particulate polyamide has a particle diameter (d50) of from 10 μm to 1,000 μm and a particle diameter dispersion degree (Dv/Dn) of not greater than 3.0, wherein Dv represents the volume average particle diameter of the particulate polyamide, and Dn represents the number average particle diameter of the particulate polyamide.

CROSS-REFERENCE TO RELATED APPLICATIONS

This patent application is based on and claims priority pursuant to 35U.S.C. §119 to Japanese Patent Application No. 2015-055551, 2015-083124,and 2016-004568, filed on Mar. 19, 2015, Apr. 15, 2015, and Jan. 13,2016, respectively, in the Japan Patent Office, the entire disclosure ofwhich is hereby incorporated by reference herein.

BACKGROUND

1. Technical Field

This disclosure relates to a particulate polyamide, and to a method forpreparing the particulate polyamide.

2. Description of the Related Art

Particulate polyamide produces good light scattering effect while havinggood absorption ability (such as oil absorption ability), and thereforeit is considered to use particulate polyamide as an adsorbent or acomponent of cosmetics such as foundation cream or cleansing cream.

In addition, polyamide 4 (i.e., nylon 4) which is a polymer of2-pyrrolidone, and polyamide 3 (i.e., nylon 3) which is a polymer of2-azetidinone can decompose in soil while having good hygroscopicproperty.

With respect to the method for preparing polyamide 4, a method includingpolymerizing 2-pyrrolidone in the presence of a basic catalyst and anacyl compound is proposed. In addition, a method in which a salt isadded during a processing to enhance the processability is alsoproposed.

SUMMARY

As an aspect of this disclosure, a particulate polyamide is providedwhich includes at least one of a polyamide 4 and a polyamide 3 and whichis porous and has a particle diameter (d50) of from 10 μm to 1,000 μmand a particle diameter dispersion degree (Dv/Dn) of not greater than3.0, wherein Dv represents the volume average particle diameter of theparticulate polyamide and Dn represents the number average particlediameter of the particulate polyamide.

As another aspect of this disclosure, a method for preparing theparticulate polyamide is provided which includes contacting a basematerial mixture, which includes a monomer including at least one of2-pyrrolidone and 2-azetidinone, and a basic polymerization catalyst,with a compressible fluid including carbon dioxide and having a densityof not less than 450 kg/m³ to melt or dissolve the base material mixturein the compressible fluid and to subject the monomer to a ring-openingpolymerization reaction.

The aforementioned and other aspects, features and advantages willbecome apparent upon consideration of the following description of thepreferred embodiments taken in conjunction with the accompanyingdrawings.

BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS

FIG. 1 is a phase diagram illustrating states of a material whentemperature and pressure are changed;

FIG. 2 is a phase diagram illustrating states of a compressible fluidfor use in producing a particulate polyamide according to an embodimentwhen temperature and pressure are changed;

FIG. 3 is a schematic view illustrating a continuous polymerizationsystem for use in producing the particulate polyamide;

FIG. 4 is a schematic view illustrating a batch polymerization systemfor use in producing the particulate polyamide;

FIG. 5 is an electron micrograph of a particulate polyamide of Example1;

FIGS. 6A and 6B illustrate a particulate material which has a circularform as illustrated in FIG. 6A when observed from such a direction thatthe area of the projected image of the particulate material is maximaland which has a non-circular form as illustrated in FIG. 6B whenobserved from such a direction that the area of the projected image ofthe particulate material is minimal;

FIGS. 7A and 7B illustrate another particulate material which has acircular form as illustrated in FIG. 7A when observed from such adirection that the area of the projected image of the particulatematerial is maximal and which has a non-circular form as illustrated inFIG. 7B when observed from such a direction that the area of theprojected image of the particulate material is minimal;

FIGS. 8A and 8B illustrate another particulate material which has acircular form as illustrated in FIG. 8A when observed from such adirection that the area of the projected image of the particulatematerial is maximal and which has a non-circular form as illustrated inFIG. 8B when observed from such a direction that the area of theprojected image of the particulate material is minimal;

FIGS. 9A and 9B illustrate another particulate material which has acircular form as illustrated in FIG. 9A when observed from such adirection that the area of the projected image of the particulatematerial is maximal and which has a non-circular form as illustrated inFIG. 9B when observed from such a direction that the area of theprojected image of the particulate material is minimal;

FIG. 10 is an electron micrograph of a particulate polyamide of Example7;

FIG. 11 is an electron micrograph of a particulate polyamide of Example8;

FIG. 12 is an electron micrograph of a particulate polyamide of Example9;

FIG. 13 is an electron micrograph of a particulate polyamide of Example10;

FIG. 14 is an electron micrograph of a particulate polyamide of Example11;

FIG. 15 is an electron micrograph of a particulate polyamide of Example12;

FIG. 16 is a graph illustrating the pore diameter distribution of theparticulate polyamide of Example 1;

FIG. 17 is a graph illustrating the pore diameter distribution of aparticulate polyamide of Example 15; and

FIG. 18 is a graph illustrating the pore diameter distribution of aparticulate polyamide of Example 17.

DETAILED DESCRIPTION

The object of this disclosure is to provide a particulate polyamide,which includes a polyamide 4 and/or a polyamide 3 and which is porouswhile having a relatively small average particle diameter and a narrowparticle diameter distribution.

Initially, the particulate polyamide of this disclosure will bedescribed.

The particulate polyamide of this disclosure includes at least one of apolyamide 4 and a polyamide 3 and is porous while having a particlediameter (d50) of from 10 to 1,000 μm and a particle diameter dispersiondegree of not greater than 3.0.

The particle diameter (d50) is the median diameter, which means acumulative 50 vol % diameter. Specifically, in the particle diameterdistribution curve (on a volume basis) of a particulate material, themedian diameter is defined as a particle diameter at which the totalvolume of particles having diameters greater than the particle diameteris equal to the total volume of particles having diameters less than theparticle diameter.

The particle diameter dispersion degree means a ratio (Dv/Dn) of thevolume average particle diameter (Dv) of a particulate material to thenumber average particle diameter (Dn) of the particulate material. Inthis regard, the mean volume diameter and the mean number diameter arearithmetic average particle diameters on a volume or number basis. Asthe particle diameter dispersion degree decreases (i.e., becomes closerto 1), the particulate material has a sharper particle diameterdistribution.

The particle diameter (d50), the mean volume diameter, and the meannumber diameter of a particulate polyamide can be measured by a methodincluding dispersing the particulate polyamide in a proper solvent (suchas water and alcohols) using a dispersing machine such as ultrasonicdispersing machines to prepare a dispersion liquid, and measuring theparticle diameter distribution of the particulate polyamide in thedispersion liquid with a particle diameter distribution measuringinstrument such as laser scattering particle size distributionanalyzers.

“Porous” means that a material has a number of fine pores therein.Whether or not a material is porous can be determined by observing thematerial with a scanning electron microscope.

The particulate polyamide of this disclosure includes at least one of apolyamide 4 and a polyamide 3.

Polyamide 4 and polyamide 3 decompose in soil, and therefore polyamide 4and polyamide 3 hardly become a burden on the environment. In addition,polyamide 4 and polyamide 3 have good hygroscopic property, andtherefore polyamide 4 and polyamide 3 are nice and soft.

In contrast, polyamide 6 and polyamide 12 which are popular polyamides,do not decompose in soil, and therefore polyamide 6 and polyamide 12become a burden on the environment.

The polyamide 4 and the polyamide 3 included in the particulatepolyamide of this disclosure is not particularly limited, and can behomopolymers, copolymers, and branched polymers. Specific examples ofthe polyamide 4 and the polyamide 3 include the following.

(1) Polymers and copolymers of 2-pyrrolidone(I-1) Polymers and copolymers of 2-pyrrolidone having a methylol groupwhich can optionally have a substituent.(I-2) Polymers and copolymers described in paragraph (I-1), which have amethylol group which can be acylated, etherified, urethanated orcarbonated, wherein the modified methylol group can optionally have afunctional group.(I-3) Polymers and copolymers described in paragraph (I-1) or (I-2),which have a linear or branched structure.(I-4) Copolymers described in any one of paragraphs (I-1) to (I-3),which are copolymers with a lactam compound or a lactone compound.(I-5) Copolymers described in paragraph (I-4), wherein the lactamcompound is ε-caprolactam.(I-6) Copolymers described in paragraph (I-4), wherein the lactonecompound is ε-caprolactone.(II-1) Polymers and copolymers of 2-pyrrolidone treated with acarbodiimide compound.(II-2) Polymers and copolymers described in paragraph (II-1), whereinthe carbodiimide compound is N,N′-dicyclohexylcarbodiimide.(II-3) Polymers and copolymers described in paragraph (II-1) or (II-2),which have a linear or branched structure.(II-4) Copolymers described in any one of paragraphs (II-1) to (II-3),which are copolymers with a lactam compound.(II-5) Copolymers described in paragraph (II-4), wherein the lactamcompound is ε-caprolactam.(II-6) Copolymers described in any one of paragraphs (II-1) to (II-3),which are copolymers with a lactone compound.(II-7) Copolymers described in paragraph (II-6), wherein the lactonecompound is ε-caprolactone.

In this regard, the decomposition property of the above-mentionedcopolymers and branched polymers and copolymers in soil oftendeteriorates.

The particle diameter (d50) of the particulate polyamide of thisdisclosure is from 10 μm to 1,000 μm, preferably from 10 μm to 100 μm,and even more preferably from 10 μm to 50 μm.

When the particle diameter (d50) is from 10 μm to 1,000 μm, theparticulate polyamide has good absorption ability while having goodhandling property. In addition, when an active ingredient is included inthe particulate polyamide so that the particulate polyamide emits theactive ingredient little by little, the particulate polyamide has anability to control the speed of emitting the active ingredient (i.e.,ability to gradually emit the active ingredient, hereinafter referred toas gradual emission controlling ability). When the particle diameter(d50) is from 10 μm to 100 μm, the gradual emission controlling abilityof the particulate polyamide can be further enhanced.

When the particle diameter (d50) of the particulate polyamide is lessthan 10 μm or greater than 1,000 μm, the handling property and thegradual emission controlling ability tend to deteriorate.

The particulate polyamide of this disclosure has a particle diameterdispersion degree of not greater than 3.0, and preferably not greaterthan 2. When the particle diameter dispersion degree is not greater than3.0, the particulate polyamide has good absorption ability while havinggood gradual emission controlling ability. When the particle diameterdispersion degree is not greater than 2, the gradual emissioncontrolling ability of the particulate polyamide can be furtherenhanced.

When the particle diameter dispersion degree is greater than 3.0, theabsorption ability and the gradual emission controlling ability tend todeteriorate.

The particulate polyamide of this disclosure is porous, and thereforethe particulate polyamide has good absorption ability. If theparticulate polyamide is not porous, the absorption ability of theparticulate polyamide deteriorates.

The particulate polyamide of this disclosure may have a substantiallyspherical form. In this application, a particulate material having “asubstantially spherical form” is defined as follows. Specifically, whenthe particulate material is observed from such a direction that the areaof the projected image of the particulate material is maximal, theparticulate material has a circular form, and in addition when theparticulate material is observed from such a direction that the area ofthe projected image of the particulate material is minimal, theparticulate material also has a circular form. Further, provided thatthe diameter (maximum diameter) of the particulate material is D1 whenthe particulate material is observed from such a direction that the areaof the projected image is maximal, and the diameter (maximum diameter)of the particulate material is D2 when the particulate material isobserved from such a direction that the area of the projected image isminimal, the following relationship is satisfied.

(D1−D2)/D1≦0.15.

The particle diameter D1 and the particle diameter D2 of a particulatematerial can be determined by observing the particulate material with ascanning electron microscope (SEM). Specifically, randomly selected 30particles of the particulate material are observed with a SEM, and theratio (D1−D2)/D1 of each particle is determined, followed by averagingthe 30 data of the ratio. When the particulate material satisfies therelationship mentioned above, the particulate material is considered asa particulate material having a substantially spherical form in thisapplication.

When the particulate polyamide of this disclosure has a non-sphericalform, the adhesiveness of the particulate polyamide is enhanced.

One preferable example of the particulate polyamide having anon-spherical form is a non-spherical particulate polyamide which has acircular form when the particulate polyamide is observed from such adirection that the area of the projected image of the particulatepolyamide is maximal and which has a non-circular form when theparticulate polyamide is observed from such a direction that the area ofthe projected image of the particulate polyamide is minimal. In thisregard, the “circular form” satisfies the following relationship:

(H1/D3)≦0.15,

wherein H1 represents the true circularity degree (defined in JIS B0621) of the projected image, and D3 represents the maximum diameter ofthe projected image. Namely, when the particulate polyamide is observedfrom such a direction that the area of the projected image of theparticulate polyamide is maximal, the maximum diameter D3 is equal tothe maximum diameter D1 mentioned above. In addition, when theparticulate polyamide is observed from such a direction that the area ofthe projected image of the particulate polyamide is minimal, the maximumdiameter D3 is equal to the maximum diameter D2 mentioned above.

The true circularity degree (H1) of a projected image is determined asthe minimum value of difference (in units of mm) between the radius of acircumscribed circle and the radius of an inscribed circle of theprojected image, wherein the circumscribed circle and the inscribedcircle are concentric circles.

Specific examples of the “non-circular form” include forms having arecessed portion, hemispherical forms, polyhedral forms, biconvex lensforms, bale forms, etc.

Specific examples of the above-mentioned non-spherical particulatematerial (polyamide) are illustrated in FIGS. 6-9.

FIG. 6A illustrates a particulate polyamide having a non-circular form,which is observed from such a direction that the area of the projectedimage of the particulate polyamide is maximal and which has a circularform, and FIG. 6B illustrates the particulate polyamide from such adirection that the area of the projected image of the particulatepolyamide is minimal and which has a non-circular form. In FIG. 6A,character A represents the maximum diameter of the particulate polyamidewhen the particulate polyamide is observed from the direction such thatthe area of the projected image of the particulate polyamide is maximal.It can be understood that the particulate polyamide illustrated in FIGS.6A and 6B is a non-spherical particulate polyamide having one recessedportion (notch).

FIGS. 7A and 7B illustrate a non-spherical particulate polyamide havingtwo recessed portions (notches).

In FIGS. 6B and 7B, characters B1, B2 and B3 represent depths of thenotches. Each of the depths B1, B2 and B3 is preferably from 0.1 A to0.9 A, wherein A represents the maximum diameter of the particulatepolyamide as described above. Characters C1, C2 and C3 represent widthsof the notches. Each of the widths C1, C2 and C3 is preferably from 0.01A to 0.95 A.

The number of notches present in one particle of the non-sphericalparticulate polyamide is preferably from 1 to 100. When two or morenotches are present, the forms of the notches may be the same as ordifferent from each other. Specifically, in FIG. 7B, the depth B2 may bethe same as or different from the depth B3, and the width C2 may be thesame as or different from the width C3.

The shape of the notch is not particularly limited, and may be a notchhaving a corner such as notches having a triangular form, a quadrangularform, etc., or a notch having no corner such as notches having asemi-circular form.

FIGS. 8A and 8B illustrate a non-spherical particulate polyamide whichhas a biconvex lens form when observed from such a direction that thearea of the projected image of the particulate material is minimal.Characters D and E represent heights of the particulate polyamide fromthe center thereof. Each of the heights D and E is preferably from 0.1 Ato 0.8 A, wherein A represents the maximum diameter of the particulatepolyamide. The height D may be the same as or different from the heightE.

FIGS. 9A and 9B illustrate a non-spherical particulate polyamide whichhas a bale form when observed from such a direction that the area of theprojected image of the particulate material is minimal. Characters F andG represent a shorter side length and a longer side length of thebale-form particulate polyamide, respectively. Each of the lengths F andG is preferably from 0.1 A to 0.8 A, wherein A represents the maximumdiameter of the particulate polyamide. The length F may be the same asor different from (less than) the length G.

The shape of a particulate polyamide can be determined by observing theparticulate polyamide with an electron microscope or the like. Inaddition, the lengths A to G can be determined from cross-sectionalslices of the particulate polyamide. Specifically, randomly selected 30particles of a particulate polyamide are observed with an electronmicroscope, and the lengths A to G of the particles are measured. Inthis regard, the number of notches present in the particulate polyamideis the average of 30 data of the 30 particles, and the length (diameter)A of the particulate polyamide is the average of 30 data of the 30particles. The length (depth) B of notches present in the particulatepolyamide is the maximum and minimum values in the data of the 30particles. In addition, the length (width) C of notches present in theparticulate polyamide is the maximum and minimum values in the data ofthe 30 particles. The cross-sectional slice can be prepared by a focusedion beam system (FIB).

The particulate polyamide of this disclosure preferably has a specificsurface area of not less than 10 m²/g, and more preferably not less than20 m²/g. When the specific surface area is not less than 10 m²/g, theabsorption ability of the particulate polyamide is enhanced.

The specific surface area can be measured by a gas absorption methodusing a nitrogen gas, and is determined as the BET(Brunauer-Emmett-Teller) specific surface area.

The particulate polyamide of this disclosure includes fine porestherein. When a curve showing a relation between the diameter (in unitsof nanometer) of pores and the frequency of the pores is described (forexample, such a curve as illustrated in FIG. 13), a pore diameter peakratio (P_(H)/P_(L)) of the value of a peak (P_(H)) in a relatively highdiameter range of not less than 100 nm to the value of a peak (P_(L)) ina relative low diameter range of not greater than 50 nm is preferablynot less than 0.7 (i.e., 70%).

The pore diameter distribution can be measured by a gas absorptionmethod, and is determined by the BJH (Barrett-Joyner-Halenda) analysismethod.

The frequency peaks (P_(H) and P_(L)) can be determined from a porediameter distribution curve on a volume basis.

The pore diameter peak ratio (P_(H)/P_(L)) is more preferably not lessthan 0.8 (80%).

The pore diameter peak ratio (P_(H)/P_(L)) can be not less than 1.0.

In order to increase the amount of a material absorbed by theparticulate polyamide and to enhance the gradual emission controllingability of the particulate polyamide, the pore diameter peak ratio(P_(H)/P_(L)) is preferably not less than 0.7 (70%).

When the pore diameter peak ratio (P_(H)/P_(L)) is less than 0.7, theabsorption ability of the particulate polyamide tends to deterioratebecause the number of relatively large pores decreases.

The particulate polyamide of this disclosure preferably has a hollowtherein, namely, the particulate polyamide preferably has a shellstructure. The shell preferably has a thickness (t) of from T/10 to T/3,wherein T represents the outer diameter of the particulate polyamide.Namely, the ratio (t/T) is preferably from 1/10 to ⅓.

The ratio (t/T) can be calculated by the following equation.

t/T=(T−h)/2/T,

wherein h represents the diameter of the hollow.

The diameter (T) of the particulate polyamide and the diameter (h) ofthe hollow can be determined by observing a cross-sectional slice, whichis prepared by a microtome, with an electron microscope. In this regard,the diameter (T) of the particulate polyamide and the diameter (h) ofthe hollow are the maximum diameters thereof when the diameters varydepending on the measurement points.

The diameters T and h are determined by averaging 30 data of 30 randomlyselected particles of the particulate polyamide.

The ratio (t/T) is preferably from 1/10 to ⅓, and more preferably from ⅛to ⅕.

When the ratio (t/T) is from 1/10 to ⅓, occurrence of a problem in thatthe particulate polyamide is easily damaged by friction because of beingbrittle can be prevented, and the particulate polyamide can bear asufficient amount of ingredient such as medical agents.

The pores in the shell of a particle of the particulate polyamidepreferably communicate with the hollow of the particle because theparticle can quickly bear a sufficient amount of ingredient. In thisregard, the pores in the shell preferably extend radially whilecommunicating with the hollow so that the particle can quickly bear asufficient amount of ingredient. Whether or not the pores communicatewith the hollow can be determined by observing a cross-sectional sliceprepared by a method such as FIB.

When the particulate polyamide has a hollow therein, the particulatepolyamide can bear an ingredient in the hollow, and therefore thespecific surface area of the particulate polyamide may be less than 10m²/g.

Next, the method of preparing the particulate polyamide of thisdisclosure will be described.

The particulate polyamide can be prepared by a method includingpreparing a base material mixture including a monomer including at leastone of 2-pyrrolidone and 2-azetidinone and a basic polymerizationcatalyst; and contacting the base material mixture with a compressiblefluid including carbon dioxide and having a density of not less than 450kg/m³ to melt the base material mixture or to dissolve the base materialmixture in the compressible fluid while subjecting the monomer toring-opening polymerization.

When a polyamide 4 is prepared by a conventional method, a problem inthat an agglomerated polyamide is formed in the polymerizing process andtherefore particles of polyamide 4 cannot be produced is caused.

As a result of the present inventors' diligent investigation, it isfound that by polymerizing 2-pyrrolidone or 2-azetidinone in acompressible fluid including carbon dioxide and having a high density, aparticulate polyamide which is porous while having a particle diameter(d50) of from 10 μm to 1,000 μm and a particle diameter dispersiondegree of not greater than 3.0 can be produced.

In order to prepare a particulate polyamide including a polyamide 4,2-pyrrolidone is used as the monomer. In order to prepare a particulatepolyamide including a polyamide 3, 2-azetidinone is used as the monomer.In order to prepare a particulate polyamide including a polyamide 4 anda polyamide 3, 2-pyrrolidone and 2-azetidinone are used as the monomer.

When the base material mixture is contacted with a compressible fluidincluding carbon dioxide and having a density of not less than 450 kg/m³so as to be melted or dissolved therein, the base material mixture isdissolved or dispersed in the compressible fluid. Therefore, the monomercan be subjected to ring-opening polymerization while dispersed in thecompressible fluid, and therefore a particulate polyamide can beprepared without forming agglomeration of polyamide.

In addition, by performing ring-opening polymerization by contacting themonomer with a compressible fluid including carbon dioxide and having adensity of not less than 450 kg/m³, the resultant polyamide becomesporous.

Further, when a compressible fluid having a density of not less than 700kg/m³, a particulate polyamide having a pore diameter peak ratio(P_(H)/P_(L)) of not less than 0.7 can be easily prepared. The densityof the compressible fluid is more preferably not less than 800 kg/m³. Inthis case, the particle diameter dispersion degree (Dv/Dn) of theparticulate polyamide can be enhanced (i.e., decreased). When thedensity is less than 450 kg/m³, the particulate polyamide tends toagglomerate (i.e., united particles of polyamide tend to be formed).

The density of the compressible fluid can be controlled by adjusting thetemperature and pressure of the compressible fluid. The temperature ofthe compressible fluid is preferably not higher than 70° C., and morepreferably not higher than 50° C. The pressure of the compressible fluidis preferably from 5 MPa to 30 MPa, and even more preferably from 20 MPato 30 MPa.

Next, the base material mixture will be described.

The base material mixture includes at least 2-pyrrolidone and/or2-azetidinone, and a basic polymerization catalyst, and optionallyincludes other components.

Suitable materials for use as the basic polymerization catalyst includecatalysts used for anionic polymerization of lactam compounds. Specificexamples of such catalysts include alkali metals (e.g., sodium,potassium and lithium), hydroxides, hydrides, oxides and salts of alkalimetals (e.g., potassium hydroxide, sodium hydride, potassium methylate,sodium methylate, sodium pyrrolidone, potassium pyrrolidone, and sodiumalkolate), hydrides of alkali earth metals (e.g., calcium hydride),basic organic metal compounds (e.g., alkyl lithium, alkyl potassium,alkyl sodium, alkyl aluminum, and n-butyl lithium), etc.

Among these compounds, metal salts of 2-pyrrolidone or 2-azetidinone arepreferable because of having good ring-opening polymerizationreactivity. Among the metal salts of 2-pyrrolidone or 2-azetidinone,alkali metal salts of 2-pyrrolidone or 2-azetidinone are morepreferable, and potassium salts of 2-pyrrolidone or 2-azetidinone (i.e.,potassium pyrrolidone and potassium azetidinone) are even morepreferable. In addition, sodium hydride is also preferable because ofhaving a good combination of handling property and polymerizationproperty.

The added amount of such a basic polymerization catalyst is notparticularly limited, but is preferably from 0.001 moles to 2 molesbased on 1 mole of the monomer used (2-pyrrolidone and/or2-azetidinone). When the added amount is in the preferable range, themonomer can polymerize quickly and the resultant polyamide has arelatively high molecular weight.

In addition, the shape of the particulate polyamide is influenced by theadded amount of the basic polymerization catalyst used. When the addedamount is less than 0.01 moles, the resultant polyamide tends to have anon-spherical form.

When the above-mentioned metal salts of 2-pyrrolidone or 2-azetidinoneare used as the basic polymerization catalyst, the base material mixturecan be prepared by reacting a metal alkoxide (e.g., alkoxides of alkalimetals such as potassium and sodium) with an excessive amount of2-pyrrolidone and/or 2-azetidinone. Among various alkoxides, alkoxideshaving 1 to 6 carbon atoms are preferable. Specific examples of thealkoxides having 1 to 6 carbon atoms include methoxides, ethoxides, andt-butoxides.

In addition, when an alkali metal salt is used as the basicpolymerization catalyst, the resultant particulate polyamide tends tohave a hollow therein.

Next, the activating agent will be described. When the particulatepolyamide is prepared, it is preferable that 2-pyrrolidone and/or2-azetidinone is subjected to ring-opening polymerization in thepresence of an activating agent because the reaction can be performed ata high reaction rate.

In this application, carbon dioxide used for the compressible fluid isnot the activating agent.

Among various activating agents, activating agents having an acyl groupare preferable. Specific examples of such activating agents includehalogenated carboxylic acids, carboxylic acid anhydrides, and carboxylicacid esters. Among these, halogenated carboxylic acids, and carboxylicacid esters are preferable.

Specific examples of such halogenated carboxylic acids includechlorinated carboxylic acids, fluorinated carboxylic acids, andbrominated carboxylic acids. Among these, chlorinated carboxylic acidsare preferable. Specific examples of such chlorinated carboxylic acidsinclude benzoyl chloride.

In addition, carboxylic acid compounds having a group derived from2-pyrrolidone and 2-azetidinone are preferable as the activating agent.Specific examples of such carboxylic acid compounds includeN-acyl-2-pyrrolidone (e.g., 1-acetyl-2-pyrrolidone) andN-acyl-2-azetidinone (e.g., 1-acetyl-2-azetidinone), which are examplesof activating agents having an acyl group.

The added amount of such an activating agent is not particularlylimited, but is preferably not less than 0.0001 moles, and morepreferably from 0.2 moles to 20 moles, based on 1 mole of the monomerused (2-pyrrolidone and/or 2-azetidinone). When the added amount is lessthan 0.02 moles, the resultant polyamide tends to have a hollow therein.

When the ring-opening polymerization is performed, an additive can beadded if desired. Specific examples of such an additive includesurfactants, antioxidants, stabilizers, antifog agents, ultravioletabsorbents, pigments, colorants, particulate inorganic materials,fillers, heat stabilizers, flame retardants, crystal nucleating agents,antistatic agents, wetting agents, incineration assisting agents,lubricants, natural materials, release agents, plasticizers, etc. Inaddition, polymerization terminators such as benzoic acid, hydrochloricacid, phosphoric acid, metaphosphoric acid, acetic acid, and lacticacid) can also be used as the additive, if desired. The added amount ofsuch an additive changes depending on the purpose and property of theadditive, but is preferably from 0 to 5 parts by weight based on 100parts by weight of the particulate polyamide.

Specific examples of the above-mentioned stabilizers include epoxydizedsoybean oils, and carbodiimide.

Specific examples of the antioxidants include2,6-di-t-butyl-4-methylphenol, and butylhydroxyanisole.

Specific examples of the antifog agents include glycerin fatty acidesters, and monostearyl citrate.

Specific examples of the fillers include clay, talc and silica, whichcan serve as an ultraviolet absorbent, a heat stabilizer, a flameretardant, an internal release agent, and a crystal nucleating agent.

Specific examples of the pigments include titanium oxide, carbon blackand ultramarine.

Next, the compressible fluid for use in preparing the particulatepolyamide of this disclosure will be described by reference to FIGS. 1and 2.

FIG. 1 is a phase diagram illustrating states of a material whentemperature and pressure are changed, and FIG. 2 is a phase diagramillustrating states of a compressible fluid used for producing a polymeraccording to an embodiment when temperature and pressure are changed. Inthis application, the compressible fluid means the fluid in any one ofthe regions (states) (1), (2) and (3) illustrated in FIG. 2.

Specific examples of the material for use as the compressible fluidinclude carbon monoxide, carbon dioxide, dinitrogen monoxide, nitrogen,methane, ethane, propane, 2,3-dimethylbutane, and ethylene.

In the method of preparing the particulate polyamide of this disclosure,the compressible fluid preferably includes carbon dioxide in an amountof not less than 50% by weight to easily prepare the particulatepolyamide.

In the region (1), (2) or (3) in FIG. 2, the material has a very highdensity, and exhibits behavior different from that at normaltemperatures and pressures. A material in the region (1) is called asupercritical fluid. The supercritical fluid means a fluid which ispresent as a non-condensable high density fluid in atemperature/pressure region over a critical point C (illustrated inFIGS. 1 and 2) under which both a gas and a liquid of the material canexist and which is not condensed even when being compressed. A materialin the region (2) is a liquid. In this embodiment, the material in theregion (2) means a liquefied gas obtained by compressing a material,which is present as a gas at normal temperature (25° C.) and pressure (1atm). A material in the region (3) is a gas. In this embodiment, thematerial in the region (3) means a high-pressure gas which has apressure not lower than ½Pc, wherein Pc represents a critical pressureand is illustrated in FIGS. 1 and 2. In FIGS. 1 and 2, characters T andTc respectively denote a triple point, and a critical temperature.

By adding such a compressible fluid to the ring-opening polymerizationsystem, the ring-opening polymerization can be performed without usingan organic solvent. In addition, the resultant polymer can be easilyextracted from the system.

Next, the polymerization reaction apparatus for use in producing theparticulate polyamide of this disclosure will be described by referenceto FIGS. 3 and 4.

Initially, a continuous polymerization reaction apparatus for use inpreparing the particulate polyamide of this disclosure will be describedby reference to FIG. 3.

FIG. 3 is a system diagram illustrating an example of the polymerizationprocess. As mentioned above, when 2-pyrrolidone and/or 2-azetidinone aresubjected to anionic polymerization by a conventional method, anagglomerated polyamide (massive polyamide) is formed in the polymerizingprocess, and therefore polyamide particles cannot be continuouslyproduced. In contrast, by using the method of this embodiment using apolymerization reaction illustrated in FIG. 3, a particulate polymer canbe continuously prepared.

The polymerization reaction apparatus 100 includes a supply unit 100 ato supply raw materials (such as the base material mixture including amonomer including 2-pyrrolidone and/or 2-azetidinone, and other rawmaterials such as the activating agent and additives) and a compressiblefluid, and a main body 100 b (i.e., a continuous polymerization device)of the polymerization reaction apparatus to polymerize the monomer (suchas 2-pyrrolidone and 2-azetidinone) supplied by the supply unit 100 a.The supply unit 100 a includes tanks 1, 3, 5, 7 and 11, measuringfeeders 2 and 4, and measuring pumps 6, 8 and 12. The main body 100 bincludes a mixer 9 arranged at an end of the main body, a feed pump 10,a reaction container 13, a measuring pump 14, and an extrusion ring 15which is arranged at the other end of the main body. In this embodiment,a device in which the compressible fluid and the raw materials (and/orthe resultant polymer) are mixed to dissolve or melt the raw materials(and the resultant polymer) is called “a mixer.” In addition, the term“melt” means that the raw materials (and/or resultant polymer) areswelled while plasticized and liquefied by being contacted with thecompressible fluid. Further, the term “dissolve” means that the rawmaterials are dissolved in the compressible fluid.

The tank 1 of the supply unit 100 a stores the base material mixtureincluding 2-pyrrolidone and/or 2-azetidinone, and a basic polymerizationcatalyst. The base material mixture may be a powder or a liquid. Thetank 3 stores a solid raw material (such as a powdery raw material and aparticulate raw material) among the activating agent and additives used,and the tank 5 stores a liquid raw material among the activating agentand additives used. The tank 7 stores the compressible fluid. In thisregard, the tank 7 may store a gas or a solid, which can be changed to acompressible fluid in a process of supply to the mixer 9 or by beingheated or pressed in the mixer 9. In this case, the gas or solid in thetank 7, which is heated or pressed in the process of supply to the mixeror in the mixer, achieves the state (1), (2) or (3) illustrated in FIG.2 in the mixer 9.

The measuring feeder 2 continuously supplies the base material mixturestored in the tank 1 to the mixer 9 while measuring the mixture. Themeasuring feeder 4 continuously supplies the solid raw material storedin the tank 3 to the mixer 9 while measuring the solid raw material. Themeasuring feeder 6 continuously supplies the liquid raw material storedin the tank 5 to the mixer 9 while measuring the liquid raw material.The measuring pump 8 continuously supplies the compressible fluid storedin the tank 7 to the mixer 9 at a predetermined pressure and apredetermined flow rate. In this regard, the term “continuous supply”means that the raw materials or the compressible fluid is supplied sothat the polymer can be continuously produced unlike a batchpolymerization reaction apparatus. Therefore, it is possible tointermittently supply the raw materials or the compressible fluid aslong as the polymer can be continuously produced. In addition, when theactivating agent and the additives used are solid, it is possible forthe polymerization reaction apparatus 100 not to have the tank 5 and themeasuring pump 6. Similarly, when the activating agent and the additivesused are liquid, it is possible for the polymerization reactionapparatus 100 not to have the tank 3 and the measuring feeder 4.

In this embodiment, the devices of the main body 100 b are connectedwith a pressure-resistant pipe 30 as illustrated in FIG. 3 to feed theraw materials, the compressible fluid, and the prepared polymer. Inaddition, each of the mixer 9, the feed pump 10, and the reactioncontainer 13 has a pipe through which the above-mentioned raw materials,etc. are fed.

The mixer 9 of the main body 100 b of the polymerization reactionapparatus continuously contacts the raw materials such as the basematerial mixture, the activating agent and the additives supplied fromthe tanks 1, 3 and 5 with the compressible fluid supplied from the tank7 to dissolve or melt the raw materials. Therefore, the mixer 9 is adevice having a pressure-resistant container. In the mixer 9, the rawmaterials are contacted with the compressible fluid, and thereby the rawmaterials are dissolved or melted. When the raw materials are dissolved,a fluidic phase is formed, and when the raw materials are melted, amolten phase is formed. In order that the reaction evenly proceeds, itis preferable that either the fluidic phase or the molten phase isformed. In this regard, in order that the reaction proceeds under acondition such that the ratio of the raw materials to the compressiblefluid is high, the base material mixture is preferably melted in themixer 9. In this embodiment, since the raw materials and thecompressible fluid are continuously supplied, the raw materials and thecompressible fluid can be contacted with each other in the mixer 9 whilemaintaining the ratio of the raw materials to the compressible fluid ata constant level, thereby making it possible to efficiently dissolve ormelt the raw materials.

The container of the mixer 9 may be a tank type container or acylindrical container. However, a cylindrical container in which the rawmaterials are supplied from one end thereof and the mixture isdischarged from another end thereof is preferable. The container of themixer 9 has an inlet 9 a from which the compressible fluid in the tank 7is supplied by the measuring pump 8, another inlet 9 b from which thebase material mixture in the tank 1 is supplied by the measuring feeder2, another inlet 9 c from which a powder in the tank 3 is supplied bythe measuring feeder 4, and another inlet 9 d from which a liquid in thetank 5 is supplied by the measuring pump 6. Each of the inlets 9 a, 9 b,9 c and 9 d has a joint connecting the container of the mixer 9 with thepipe through which the raw materials or the compressible fluid is fed.The joint is not particularly limited, and any known joints such asreducer joints, coupling joints, Y joints, T joints, and outlet jointscan be used. In addition, the mixer 9 has a heater 9 e to heat the rawmaterials and the compressible fluid supplied. Further, the mixer 9 canhave a stirrer to stir the raw materials and the compressible fluid.Specific examples of such a stirrer include single screw stirrers, twinscrew stirrers in which two screws are engaged with each other, twoshaft mixers having multiple stirring members engaged or overlappingwith each other, kneaders having spiral stirring members engaged witheach other, and static mixers. Among these, two- or more-shaft stirrersin which the stirring members are engaged with each other are preferablebecause the amount of the reaction product adhered to the stirrers orthe container is small, and the stirrers have self-cleaning property.

When the mixer 9 has no stirrer, a pressure-resistant pipe is preferablyused as the mixer. In this case, it is preferable that the pipe has aspiral form or is folded to reduce the installation space of thepolymerization reaction apparatus 100 or to enhance the flexibility inlayout of the apparatus. In addition, when the mixer 9 has no stirrer,it is preferable that the mixture of the raw materials supplied to themixer 9 is previously liquefied so that the raw materials can be wellmixed in the mixer.

The feed pump 10 feeds the raw materials, which are dissolved or meltedin the mixer 9, to the reaction container 13. The tank 11 stores theactivating agent. The measuring pump 12 supplies the activating agentstored in the tank 11 to the reaction container 13 while measuring theactivating agent.

The reaction container 13 is a pressure-resistant container in which thedissolved or melted raw materials fed by the feed pump 10 and theactivating agent supplied by the measuring pump 12 are mixed tocontinuously subject the monomer (2-pyrrolidone and/or 2-azetidinone) toring-opening polymerization. The reaction container 13 can be a tanktype container or a cylindrical container, but is preferably acylindrical container because of having relatively small dead space.

The reaction container 13 has an inlet 13 a from which the materialsmixed in the mixer 9 are supplied to the reaction container, and anotherinlet 13 b from which the activating agent in the tank 11 is supplied bythe measuring pump 12. Each of the inlets 13 a and 13 b has a jointconnecting the reaction container 13 with the pipe through which the rawmaterials are fed. The joint is not particularly limited, and any knownjoints such as reducer joints, coupling joints, Y joints, T joints, andoutlet joints can be used.

The reaction container 13 can have a gas outlet from which a vaporizedmaterial is removed. In addition, the reaction container 13 has a heater13 c to heat the raw materials supplied. Further, the reaction container13 can have a stirrer to stir the raw materials and the compressiblefluid. When the reaction container 13 has a stirrer, it can be preventedthat the produced polymer precipitates in the reaction container due tothe difference in density between the raw materials and the polymer, andthereby the polymerization reaction can be evenly performed in aquantitative way.

Suitable stirrers for use as the stirrer of the reaction container 13include stirrers having screws engaged with each other, stirrers having2-flight (oval-shaped) or 3-flight (triangular shape) stirring members,and two- or more-shaft stirrers having a disk-shaped ormultilobar-shaped stirring blade (e.g., cloverleaf stirring blade).These stirrers have good self-cleaning property. When the raw materialsincluding the catalyst are previously mixed well, a static mixer whichcan perform separation and confluence of flow in a multistep way using aguiding device can be used as the stirrer. Specific examples of thestatic mixer include multi-stratification mixers disclosed inJP-S47-15526-B, JP-S47-15527-B and JP-S47-15528-B, KENICS MIXERSdisclosed in JP-S47-33166-A, and other mixers having no moving member.In addition, examples of the static mixer are disclosed in U.S. Pat.Nos. 4,408,893, 5,944,419 and 5,851,067 incorporated by reference.

When the reaction container 13 has no stirrer, a pressure-resistant pipeis preferably used for the reaction container. In this case, it ispreferable that the pipe has a spiral form or is folded to reduce theinstallation space of the polymerization reaction apparatus 100 or toenhance the flexibility in layout of the apparatus.

The polymerization reaction apparatus 100 illustrated in FIG. 3 includesonly one reaction container 13. However, the number of the reactioncontainer is not limited thereto, and two or more reaction containerscan be used therefor. When multiple reaction containers 13 are used, theconditions (e.g., temperature, pressure, concentration of the catalyst,average retention time, and stirring speed) of the reactions performedin the reaction containers may be the same. However, it is preferablethat the conditions are changed so as to be proper depending on theprogression of the reactions in the reaction containers. It is notpreferable that too many reaction containers are connected because thereaction time is increased and the apparatus is complicated, and thenumber of the reaction containers (i.e., the number of reaction steps)is preferably from 1 to 4, and more preferably from 1 to 3.

The measuring pump 14 discharges a particulate polyamide P from anoutlet (the extrusion ring 15 in FIG. 3) of the reaction container 13.In this regard, it is possible to discharge the particulate polyamide Pfrom the reaction container 13 without using the measuring pump 14 byutilizing pressure difference between the inside of the reactioncontainer and the outside thereof. In this case, in order to adjust thepressure in the reaction container 13 and the amount of the particulatepolyamide P discharged from the reaction container, a pressure controlvalve can be used instead of the measuring pump 14.

In order that the raw materials are efficiently melted, the time atwhich heat applied to the raw materials and the compressible fluid inthe reaction container 13 or the time at which the raw materials and thecompressible fluid in the reaction container 13 are stirred may beadjusted. In this regard, heating and stirring can be performed aftercontacting the raw materials with the compressible fluid or whilecontacting the raw materials with the compressible fluid.

Next, a batch polymerization reaction apparatus 200 will be described byreference to FIG. 4. FIG. 4 is a system diagram illustrating a batchpolymerization system for use in producing the particulate polyamide ofthis disclosure.

Referring to FIG. 4, the polymerization reaction apparatus 200 includesa tank 21, a measuring pump 22, an addition pot 25, a reaction container27, and valves 23, 24, 26, 28 and 29. These devices are connected withthe pressure-resistant pipe 30. In addition, joints 30 a and 30 b areprovided on the pipe 30.

The tank 21 stores a compressible fluid. The tank 21 can store a gas ora solid, which can be changed to a compressible fluid by being heated orpressed in a passage to the reaction container 27 or in the reactioncontainer 27. In this case, when the gas or solid stored in the tank 21is heated or pressed, the gas or solid achieves the state (1), (2) or(3) illustrated in FIG. 2 in the reaction container 27.

A measuring pump 22 supplies the compressible fluid stored in the tank21 to the reaction container 27 at a predetermined pressure and apredetermined flow rate. An addition pot 25 stores an activating agentto be added to the raw materials in the reaction container 27. Thevalves 23, 24, 26 and 29 perform switching between a passage throughwhich the compressible fluid in the tank 21 is fed to the reactioncontainer 27 via the addition pot 25, and a passage through which thecompressible fluid in the tank 21 is fed to the reaction container 27without passing through the addition pot 25, or the like switching.

Before starting polymerization, the base material mixture is containedin the reaction container 27. The reaction container 27 is apressure-resistant container in which the base material mixturepreviously contained in the container is contacted with the compressiblefluid supplied from the tank 21 and the activating agent supplied fromthe addition pot 25 to subject the monomer (2-pyrrolidone and/or2-azetidinone) to ring-opening polymerization. The reaction container 27can have a gas outlet from which a vaporized material is removed. Inaddition, the reaction container 27 has a heater to heat the rawmaterials and the compressible fluid. Further, the reaction container 27has a stirrer to stir the raw materials and the compressible fluid toprevent occurrence of a problem in that the produced polymerprecipitates in the reaction container due to difference in densitybetween the raw materials and the polymer, and therefore thepolymerization reaction can be evenly performed in a quantitative way.The valve 28 has a function of discharging the particulate polyamide Pfrom the reaction container 27 when the valve is opened after thepolymerization reaction is completed.

Next, the method of preparing the particulate polyamide using theabove-mentioned raw materials, the compressible fluid, and thepolymerization reaction apparatus 100, which is an example of thepolymerization reaction apparatus, will be described. According to themethod, the base material mixture including a monomer including2-pyrrolidone and/or 2-azetidinone, and a basic polymerization catalystare contacted with the compressible fluid to melt or dissolve the basematerial mixture in the compressible fluid and to subject the monomer toring-opening polymerization.

Initially, the measuring feeders 2 and 4 and the measuring pumps 6 and 8are operated to continuously supply the base material mixture, thecompressible fluid, and optional activating agent and additives, whichare stored in the tanks 1, 3, 5 and 7, to the mixer 9 through therespective inlets 9 a, 9 b, 9 c and 9 d. In general, accuracy ofmeasuring a solid (powdery or particulate material) is relatively lowcompared to accuracy of measuring a liquid. Therefore, when a solid rawmaterial is used, it is preferable that the solid raw material is heatedto a temperature higher than the melting point of the raw material sothat the liquefied raw material is contained in the tank 5 so as to besupplied to the mixer 9 by the measuring pump 6. The order of activationof the measuring feeders 2 and 4 and the measuring pumps 6 and 8 is notparticularly limited, but it is preferable that the measuring pump 8 isinitially activated because when the raw materials are fed to thereaction container 13 without being contacted with the compressiblefluid, the raw materials may be solidified due to drop in temperature ofthe raw materials and the reaction is unevenly performed.

The supplying speeds at which the raw materials are supplied by themeasuring feeders 2 and 4 and the measuring pump 6 are controlled basedon the ratio of the base material mixture, the activating agent, and theadditives so that the ratio of the raw materials becomes a predeterminedratio. Specifically, the total weight of the raw materials supplied bythe measuring feeders 2 and 4 and the measuring pump 6 per a unit time(i.e., supplying speed of raw materials in units of g/min) is adjustedbased on factors such as the desired property of the polymer and thereaction time. Similarly, the weight of the compressible fluid suppliedby the measuring pump 8 per a unit time (i.e., supplying speed ofcompressible fluid in units of g/min) is also adjusted based on factorssuch as the desired property of the polymer and the reaction time. Theratio Sr/Sc (feed ratio) of the supplying speed (Sr) of the rawmaterials to the supplying speed (Sc) of the compressible fluid is notparticularly limited, and is properly determined.

The mixing ratio of the weight (Wm) of the monomer to the weight (Wc) ofthe compressible fluid, which mixing ratio is defined by thebelow-mentioned equation (1), is preferably not greater than 0.3.

Mixing ratio=Wm/(Wm+Wc)  (1).

The mixing ratio is more preferably from 0.001 to 0.3, and even morepreferably from 0.01 to 0.3.

Since the raw materials and the compressible fluid are continuouslysupplied to the container of the mixer 9, the raw materials and thecompressible fluid are continuously contacted with each other.Therefore, the raw materials such as the base material mixture, theactivating agent, and the additives are dissolved or melted in thecompressible fluid in the mixer 9. In this regard, when the mixer 9 hasa stirrer, the raw materials and the compressible fluid may be stirred.In order to prevent the supplied compressible fluid from changing to agas, the temperature and the pressure in the reaction container 13 arecontrolled so as to be a temperature and a pressure not lower than thoseof the fluid at the triple point T illustrated in FIGS. 1 and 2. In thisregard, the pressure can be controlled by adjusting the flow rate of thepumps, the diameter, length and shape of the tubes. In addition, thiscontrol can be performed by adjusting the output of the heater 9 e ofthe mixer 9 or the supplying speed of the compressible fluid.

In order that the raw materials can be efficiently mixed, the timing ofheating and stirring the raw materials and the compressible fluid can beadjusted. In this regard, a method in which after the raw materials arecontacted with the compressible fluid, heating and stirring areperformed thereon, or a method in which the raw materials are contactedwith the compressible fluid while heating and stirring are performedthereon can be used. In addition, in order to securely mix the rawmaterials, a method in which after the base material mixture is heatedto a temperature not lower than the melting point thereof, the mixtureis contacted with the compressible fluid can be used. For example, whenthe mixer 9 is a two shaft mixer having screws, the above-mentionedconditions can be satisfied by adjusting the arrangement of the screws,the arrangement of the inlets 9 a, 9 b, 9 c and 9 d, and the temperatureof the heater 9 e of the mixer.

In this embodiment, the additives are supplied to the mixer 9 separatelyfrom the base material mixture. However, the additives can be suppliedtogether with the base material mixture. In addition, it is possiblethat after the polymerization reaction, the additives are supplied tothe resultant polymer. In this regard, it is possible that after theparticulate polyamide P is discharged from the reaction container 13,the additives are added to the polyamide.

The raw materials mixed in the mixer 9 are supplied by the feed pump 10to the reaction container 13 through the inlet 13 a.

The raw materials supplied to the reaction container 13 are fullystirred by the stirrer of the reaction container if desired. Inaddition, if desired, the raw materials are heated to a predeterminedtemperature (polymerization reaction temperature) by the heater 13 ewhen being fed. Therefore, the monomer (2-pyrrolidone and/or2-azetidinone) is subjected to ring-opening polymerization in thereaction container 13 in the presence of the activating agent (i.e., thepolymerization process is performed). The polymerization reactiontemperature of the ring-opening polymerization of the monomer is notparticularly limited, and is properly determined. However, the reactionpolymerization temperature is preferably from 40° C. to 70° C. When thepolymerization reaction temperature is in the preferable range, problemssuch that the reaction speed deteriorates; and a side reaction is madehardly occur. The polymerization reaction temperature can be controlled,for example, by heating the polymerization reaction apparatus with aheater, which is provided on the apparatus, or an external heater.

In this embodiment, the polymerization reaction time (i.e., averageresidence time of the raw materials in the reaction container 13) isdetermined depending on the target molecular weight of the polymer. Whenthe target molecular weight is from 5,000 to 10,000,000, thepolymerization reaction time is generally from 30 minutes to 120minutes.

The polymerization reaction time influences the shape of the particulatepolyamide, and when the polymerization reaction time is relativelyshort, non-spherical particles having a notch tends to be produced.

The particulate polyamide P formed in the reaction container 13 by thering-opening reaction is discharged from the reaction container 13 bythe measuring pump 14. The measuring pump 14 preferably feeds theparticulate polyamide P at a constant speed so that the pressure in thereaction container 13 filled with the compressible fluid becomesconstant, and thereby the polymerization reaction is evenly performed,resulting in production of a homogeneous particulate polyamide.Therefore, the liquid feeding mechanism of the reaction container 13 andthe liquid feeding rate of the feed pump 10 are controlled so that theback pressure of the measuring pump 14 becomes constant. Similarly, inorder that the back pressure of the feed pump 10 becomes constant, theliquid feeding mechanism of the mixer 9 and the feeding speeds of themeasuring feeders 2 and 4 and the measuring pumps 6 and 8 arecontrolled. In this regard, ON-OFF control methods (i.e., intermittentfeeding methods) can be used for the control method, but continuous orstep-by-step methods in which the rotation speed of the pumps, etc., isgradually increased or decreased are often preferably used. By usingsuch control methods, a homogeneous particulate polyamide can be stablyproduced.

The thus prepared particulate polyamide P is optionally subjected to atreatment in which the monomer and catalyst remaining in the polymer areremoved therefrom. The removing method used for the treatment is notparticularly limited, but an extraction method using decompressiondistillation or using a compressible fluid, or a water washing methodcan be used. When an extraction method using decompression distillationis used, the decompression conditions are determined depending on theboiling point of the catalyst used. In an extraction method using acompressible fluid, after the polymerization reaction, the compressiblefluid used is discharged, and the particulate polyamide is contactedwith a new compressible fluid, wherein this washing operation ispreferably performed plural times.

The pressure of the reaction system in the polymerization reaction(i.e., the pressure of the compressible fluid) may be the pressure atwhich the compressible fluid supplied from the tank 7 becomes aliquefied gas (i.e., the state (2) in FIG. 2) or a high pressure gas(i.e., the state (3) in FIG. 2), but is preferably the pressure at whichthe compressible fluid becomes a supercritical fluid (i.e., the state(1) in FIG. 2). When the compressible fluid is in the supercriticalfluid state, melting of the base material mixture can be accelerated,and thereby the polymerization reaction can be evenly performed in aquantitative way.

The weight average molecular weight of the thus prepared polymer ispreferably from 1,000 to 5,000,000.

The particulate polyamide of this disclosure can be used, for example,for cosmetics, adsorbents, catalyst bearers, electronic devices (e.g.,displays), and chromatography.

Having generally described this invention, further understanding can beobtained by reference to certain specific examples which are providedherein for the purpose of illustration only and are not intended to belimiting. In the descriptions in the following examples, the numbersrepresent weight ratios in parts, unless otherwise specified.

EXAMPLES

In the following example, the density of the compressible fluid, theweight average molecular weight of the polymers prepared, and theparticle diameter, particle diameter dispersion degree, specific surfacearea and pore diameter distribution of the particulate polyamideprepared were measured by the following methods.

1. Method for Measuring Density of Compressible Fluid

The density of the compressible fluid was measured based on the method,which is described in detail in “A new equation of state for carbondioxide covering the fluid region from the triple point temperature to1100K at pressures up to 800 MPa” by R. Span and W. Wagner, J. Phys.Chem. Ref. Data 25, pp. 1509-1596 (1996), incorporated herein byreference.

2. Weight average molecular weight of particulate polyamide

The weight average molecular weight was measure by gel permeationchromatography (GPC) under the following conditions.

Measuring instrument: HLC-8220GPC from TOSOH CORPORATION

Column: TSK GMH_(HR) from TOSOH CORPORATION

Temperature: 40° C.

Solvent: 5 mmol/l hexafluoroisopropanol solution of sodiumtrifluoroacetate

Flow rate: 0.2 ml/min

Initially, 1 ml of 0.05% by weight of a polymer solution was injectedinto the measuring instrument to measure the molecular weightdistribution of the polymer under the above-mentioned conditions. Theweight average molecular weight (Mw) of the polymer was calculated basedon the molecular weight calibration curve, which was prepared by usingmonodisperse polymethyl methacrylates (PMMA).

3. Particle Diameter (d50) of Particulate Polyamide

The particle diameter (d50) was measured using a Laser ScatteringParticle Size Distribution Analyzer LA-920 from Horiba Ltd.Specifically, a particulate polyamide was mixed with water and themixture was subjected to a supersonic dispersing treatment for 10minutes to prepare a sample. The sample was set in the measuringinstrument to determine the particle diameter (d50) of the particulatepolyamide.

4. Particle Diameter Dispersion Degree of Particulate Polyamide

The particle diameter dispersion degree (Dv/Dn) of a particulatepolyamide was calculated from the volume average particle diameter (Dv)and the number average particle diameter (Dn) of the particulatepolyamide, which were measured by the Laser Scattering Particle SizeDistribution Analyzer LA-920.

5. Specific Surface Area and Pore Diameter Distribution of ParticulatePolyamide

The specific surface area and pore diameter distribution of aparticulate polyamide were measured by a surface area and porosityanalyzer TRISTAR 3020 from Shimadzu Corp. In addition, the pore diameterpeak ratio (P_(H)/P_(L)) of the value of a peak (P_(H)) in a relativelyhigh diameter range of not less than 100 nm to the value of a peak(P_(L)) in a relative low diameter range of not greater than 50 nm wasdetermined by the BJH analysis method mentioned above.

The sample was subjected to reduce-pressure drying for 12 hours beforemeasuring the specific surface area and pore diameter distribution.

6. Adhesiveness of Particulate Polyamide

The particulate polyamides of Examples 7 to 12 were evaluated withrespect to adhesiveness.

Specifically, a particulate polyamide was spread on a surface of a glassplate, which was coated with an acrylic binder (DIANAL BR-116 fromMitsubishi Rayon Co., Ltd.), so that the particulate polyamide adheresto the surface of the glass plate.

After the surface was rubbed with a cloth 20 times in a back and forthmanner using a rubbing tester, the surface of the glass plate wasobserved to determine whether or not particles of the particulatepolyamide are released from the surface.

The adhesiveness was evaluated by the following method.

⊚: The percentage of particles released from the surface (i.e., the areaof the surface from which particles of the particulate polyamide arereleased) is not greater than 10%.◯: The percentage of particles released from the surface is greater than10% and not greater than 30%.Δ: The percentage of particles released from the surface is greater than30% and not greater than 50%.

7. Gradual Emission Controlling Ability of Particulate Polyamide

The particulate polyamides of Examples 1 and 13 to 17 were evaluatedwith respect to the gradual emission controlling ability.

Initially, 100 parts by weight of a particulate polyamide and 104 partsby weight of squalane were mixed by a desk-top mixer, and the resultantmixture was further mixed by a HENSCHEL MIXER mixer. Next, a liquidparaffin, which had been heated so as to be melted, was added to themixture. The mixture was then kneaded by a roll mill. The kneadedmixture was heated while stirred to be melted, and then cooled to 30°C., followed by adding a fragrance thereto. The mixture was poured intoa metal dish, and then cooled to prepare an oil-based foundation.

Next, 500 mg of the oil-based foundation, which was precisely weighed,was added into 500 ml of refined water, and the mixture was allowed tosettle at 20° C. After 1 hour, 5 hours, 10 hours, and 15 hours ofmixing, the eluate was sampled, and filtered to remove the particulatematerial therefrom. Next, the concentration of the ingredient (i.e.,squalane) in the elute was measured by high-performance liquidchromatography to determine the dissolution rate of squalane. Theresults are shown in Table 3 below.

In this regard, the dissolution rate described in Table 3 is determinedby the following equation.

Dissolution rate (%)=(W2/W1)×100,

wherein W1 represents the ingredient (squalane) bearing amount of theparticulate polyamide, and W2 represents the amount of the ingredient(squalane) in the eluate.

8. Ingredient Bearing Ability

The particulate polyamides of Examples 1 and 13 to 17 were evaluatedwith respect to the ingredient bearing amount (i.e., the amount ofingredient which the particulate polyamide can bear therein).

The ingredient bearing ability of the particulate polyamide wascalculated from the above-mentioned ingredient bearing amount, which wasmeasured by high-performance liquid chromatography.

The ingredient bearing ability is determined by the following equation.

Ingredient bearing ability=(W1/W)×100(% by weight),

wherein W represents the weight of the particulate polyamide, and W1represents the ingredient (squalane) bearing amount of the particulatepolyamide (i.e., the amount of ingredient which the particulatepolyamide bears therein).

The ingredient bearing ability is graded as follows.

⊚: The ingredient bearing ability is not less than 30% by weight.◯: The ingredient bearing ability is not less than 20% by weight.Δ: The ingredient bearing ability is not less than 10% by weight.X: The ingredient bearing ability is less than 10% by weight.

Example 1

The following components were fed into a flask equipped with adecompressing device.

2-Pyrrolidone (which was refined to remove 21.3 g (0.25 mol) watertherefrom) Potassium t-butoxide serving as a catalyst 0.346 g (3 mmol)

The mixture was heated to 50° C. to react the catalyst. As a result, amixture of 2-pyrrolidone and a potassium salt of 2-pyrrolidone wasobtained.

Next, the ring-opening polymerization of 2-pyrrolidone was performedusing the polymerization reaction apparatus 200 illustrated in FIG. 4.The configuration of the polymerization reaction apparatus 200 was thefollowing.

Tank 21: carbon dioxide (CO₂) bottle

Addition pot 25: ¼-inch SUS 316 pipe sandwiched by the valves 24 and 29was used as the addition pot. The addition pot was preliminarily filledwith 0.54 g of an activating agent 1-acetyl-2-pyrrolidone.

Reaction container 27: A 100 ml pressure resistant SUS 316 container wasused as the reaction container. The reaction container was preliminarilyfilled with 12.15 g of the base material mixture.

The measuring pump 22 was operated while the valves 23 and 26 wereopened to directly supply carbon dioxide stored in the tank 21 to thereaction container 27 without using the addition pot 25. The temperatureinside the reaction container 27 was controlled at 40° C., and carbondioxide was fed into the reaction container in an amount such that thepressure of carbon dioxide becomes 6 MPa to melt the base materialmixture. Next, the valve 23 was closed and the measuring pump 22 wasoperated. When the pressure between the measuring pump 22 and the valve24 became higher than the pressure in the reaction container 27, thevalves 24 and 29 were opened to supply 1-acetyl-2-pyrrolidone in theaddition pot 25 to the reaction container 27. Further, after thepressure in the reaction container 27 was increased to 9 MPa, thepolymerization reaction of 2-pyrrolidone was performed in the reactioncontainer for 120 minutes. After the polymerization reaction, the valve28 was opened.

Next, carbon dioxide was fed again into the reaction container, and thenthe pressure in the reaction container was increased to 9 MPa, followedby opening the valve 28.

The particulate polyamide in the reaction container 27 was washed withwater, and then the particulate polyamide was extracted from thereaction container, followed by drying the particulate polyamide.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 1 are shown in Table 1 below. In addition, anelectron microscope photograph of the particulate polyamide of Example 1is shown in FIG. 5, wherein a 2 μm scale is illustrated in thephotograph. As can be understood from FIG. 5, the particulate polyamideof Example 1 was porous.

The ratio H1/D3 of the particulate polyamide when the particulatepolyamide is observed from such a direction that the area of theprojected image is maximal, and the ratio H1/D3 of the particulatepolyamide when the particulate polyamide is observed from such adirection that the area of the projected image is minimal were 0.03 atmaximum, and therefore the particulate polyamide had a circular formwhen observed from each of the directions. In this regard, H1 representsthe true circularity degree (defined in JIS B 0621) of the projectedimage, and D3 represents the maximum diameter of the projected image.When the relationship (H1/D3)≦0.15 is satisfied, the particulatepolyamide has a circular form.

In addition, the ratio (D1−D2)/D1 was 0.06, wherein D1 represents themaximum diameter of the particulate polyamide when the particulatepolyamide is observed from such a direction that the area of theprojected image is maximal, and D2 represents the maximum diameter ofthe particulate material when the particulate polyamide is observed fromsuch a direction that the area of the projected image is minimal, andtherefore the particulate polyamide has a spherical form.

The shell of particulate polyamide of Example 1 had a thickness of T/2,wherein T represents the outer diameter of the particulate polyamide,and therefore the particulate polyamide had no hollow therein (i.e., theparticulate polyamide was a solid particle).

The pore diameter distribution of the particulate polyamide of Example 1is illustrated in FIG. 16. It can be understood from FIG. 16 that thepore diameter peak ratio (P_(H)/P_(L)) of the value of a peak (P_(H)) ina relatively high diameter range of not less than 100 nm to the value ofa peak (P_(L)) in a relatively low diameter range of not greater than 50nm is 0.61 (61%).

Example 2

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the polymerization temperature and thepolymerization pressure were changed as described in Table 1 to preparea particulate polyamide of Example 2.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 2 are shown in Table 1 below.

Example 3

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the polymerization temperature and thepolymerization pressure were changed as described in Table 1 to preparea particulate polyamide of Example 3.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 3 are shown in Table 1.

Example 4

The procedure for preparation of the particulate polyamide of Example 1was repeated except that 2-pyrrolidone was replaced with 2-azetidinoneto prepare a particulate polyamide of Example 4.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 4 are shown in Table 1.

Example 5

The procedure for preparation of the particulate polyamide of Example 1was repeated except that 2-pyrrolidone was replaced with a mixture of2-pyrrolidon and 2-azetidinone in a weight ratio of 1/1 to prepare aparticulate polyamide of Example 5.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 5 are shown in Table 1.

Example 6

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the polymerization temperature, thepolymerization pressure and the mixing ratio of the monomer to thecompressible fluid were changed as described in Table 1 to prepare aparticulate polyamide of Example 6.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 6 are shown in Table 1.

Example 7

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the added amount of the activating agent, thepolymerization pressure and the mixing ratio of the monomer to thecompressible fluid were changed as described in Table 2 to prepare aparticulate polyamide of Example 7.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 7 are shown in Table 2 below. In addition, anelectron microscope photograph of the particulate polyamide of Example 7is shown in FIG. 10, wherein a 5.00 μm scale is illustrated in thephotograph. As can be understood from FIG. 10, the particulate polyamideof Example 7 was porous.

Example 8

The procedure for preparation of the particulate polyamide of Example 6was repeated except that the added amount of the activating agent, thepolymerization temperature, the polymerization pressure and the mixingratio of the monomer to the compressible fluid were changed as describedin Table 2 to prepare a particulate polyamide of Example 8.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 8 are shown in Table 2. In addition, an electronmicroscope photograph of the particulate polyamide of Example 8 is shownin FIG. 11, wherein a 10.0 μm scale is illustrated in the photograph. Ascan be understood from FIG. 11, the particulate polyamide of Example 8was porous.

The ratio (H1/D3) of the particulate polyamide was 0.14 when theparticulate polyamide was observed from such a direction that the areaof the projected image is maximal, and therefore the particulatepolyamide had a circular form when observed from the direction.

When the particulate polyamide was observed from such a direction thatthe area of the projected image is minimal, the particulate polyamidehad such a form as illustrated in FIG. 7B, i.e., a form having notches,wherein the number of notches was 38, the maximum diameter A was 21.9μm, the maximum and minimum values of the depths of the notches Bn(n=2-39) were 17.6 μm and 4.3 μm, respectively, and the maximum andminimum values of the widths of the notches Cn (n=2-39) were 3.3 μm and0.2 μm, respectively.

Example 9

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the added amount of the activating agent, theadded amount of the catalyst, the polymerization pressure, thepolymerization time and the mixing ratio of the monomer to thecompressible fluid were changed as described in Table 2 to prepare aparticulate polyamide of Example 9.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 9 are shown in Table 2. In addition, an electronmicroscope photograph of the particulate polyamide of Example 9 is shownin FIG. 12, wherein a 10.0 μm scale is illustrated in the photograph. Ascan be understood from FIG. 12, the particulate polyamide of Example 9was porous.

The ratio (H1/D3) of the particulate polyamide was 0.05 when theparticulate polyamide was observed from such a direction that the areaof the projected image is maximal, and therefore the particulatepolyamide had a circular form when observed from the direction.

When the particulate polyamide was observed from such a direction thatthe area of the projected image is minimal, the particulate polyamidehad such a form as illustrated in FIG. 6B, i.e., a form having onenotch, wherein the maximum diameter A was 15.8 μm, the depth of thenotch B1 was 8.3 μm, and the width of the notch C1 was 7.7 μm.

Example 10

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the added amount of the activating agent, theadded amount of the catalyst and the mixing ratio of the monomer to thecompressible fluid were changed as described in Table 2 to prepare aparticulate polyamide of Example 10.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 10 are shown in Table 2. In addition, an electronmicroscope photograph of the particulate polyamide of Example 10 isshown in FIG. 13, wherein a 10.0 μm scale is illustrated in thephotograph. As can be understood from FIG. 13, the particulate polyamideof Example 10 was porous.

The ratio (H1/D3) of the particulate polyamide was 0.08 when theparticulate polyamide was observed from such a direction that the areaof the projected image is maximal, and therefore the particulatepolyamide had a circular form when observed from the direction.

When the particulate polyamide was observed from such a direction thatthe area of the projected image is minimal, the particulate polyamidehad such a form as illustrated in FIG. 8B, i.e., a biconvex lens form,wherein the maximum diameter A was 12.3 μm, and the heights D and E were4.4 μm and 5.1 μm, respectively.

Example 11

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the added amount of the activating agent, theadded amount of the catalyst, the polymerization pressure and the mixingratio of the monomer to the compressible fluid were changed as describedin Table 2 to prepare a particulate polyamide of Example 11. In thisregard, the polymerization pressure was changed so as to be 9 MPa in anearlier time period of from 0 minute to 60 minutes and 30 MPa in a latertime period of from 60 minutes to 120 minutes.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 11 are shown in Table 2. In addition, an electronmicroscope photograph of the particulate polyamide of Example 11 isshown in FIG. 14, wherein a 5.00 μm scale is illustrated in thephotograph. As can be understood from FIG. 14, the particulate polyamideof Example 11 was porous.

The ratio (H1/D3) of the particulate polyamide was 0.07 when theparticulate polyamide was observed from such a direction that the areaof the projected image is maximal, and therefore the particulatepolyamide had a circular form when observed from the direction.

When the particulate polyamide was observed from such a direction thatthe area of the projected image is minimal, the particulate polyamidehad such a form as illustrated in FIG. 9B, i.e., a bale form, whereinthe maximum diameter A was 10.1 μm, and the lengths G and F were 10.1 μmand 5.8 μm, respectively.

Example 12

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the added amount of the activating agent, theadded amount of the catalyst, the polymerization pressure and the mixingratio of the monomer to the compressible fluid were changed as describedin Table 2 to prepare a particulate polyamide of Example 12.

The reaction conditions and the evaluation results of the particulatepolyamide of Example 12 are shown in Table 2. In addition, an electronmicroscope photograph of the particulate polyamide of Example 12 isshown in FIG. 15, wherein a 5.00 μm scale is illustrated in thephotograph. As can be understood from FIG. 15, the particulate polyamideof Example 12 was porous.

The ratio (H1/D3) of the particulate polyamide was 0.15 when theparticulate polyamide was observed from such a direction that the areaof the projected image is maximal, and therefore the particulatepolyamide had a circular form when observed from the direction.

When the particulate polyamide was observed from such a direction thatthe area of the projected image is minimal, the particulate polyamidehad such a form as illustrated in FIG. 7B, i.e., a form having notches,wherein the number of notches was 12, the maximum diameter A was 16.1μm, the maximum and minimum values of the depths of the notches Bn(n=2-13) were 3.3 μm and 0.2 μm, respectively, and the maximum andminimum values of the widths of the notches Cn (n=2-13) were 5.4 μm and0.8 μm, respectively.

Examples 13 to 17

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the added amount of the activating agent, theadded amount of the catalyst, the polymerization temperature and thepolymerization pressure were changed as described in Table 3 to prepareparticulate polyamides of Examples 13 to 17.

The reaction conditions and the evaluation results of the particulatepolyamides of Examples 13 to 17 are shown in Table 3 below.

Each of the particulate polyamides of Examples 13 to 17 had a hollow anda shell while having pores in the shell communicating with the hollow.

The pore diameter distribution of the particulate polyamide of Example15 is illustrated in FIG. 17. It can be understood from FIG. 17 that thepore diameter peak ratio (P_(H)/P_(L)) of the value of a peak (P_(H)) ina relatively high diameter range of not less than 100 nm to the value ofa peak (P_(L)) in a relatively low diameter range of not greater than 50nm is 0.94 (94%).

The pore diameter distribution of the particulate polyamide of Example17 is illustrated in FIG. 18. It can be understood from FIG. 18 that thepore diameter peak ratio (P_(H)/P_(L)) of the value of a peak (P_(H)) ina relatively high diameter range of not less than 100 nm to the value ofa peak (P_(L)) in a relatively low diameter range of not greater than 50nm is 1.28 (128%).

Comparative Example 1

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the raw materials were not contacted with thecompressible fluid to prepare a polyamide of Comparative Example 1. Thepolyamide of Comparative Example 1 was not particulate and had a massiveform.

The reaction conditions and the evaluation results of the particulatepolyamide of Comparative Example 1 are shown in Table 4 below.

Comparative Example 2

The procedure for preparation of the particulate polyamide of Example 1was repeated except that the polymerization temperature and thepolymerization pressure were changed as described in Table 4 below toprepare a particulate polyamide of Comparative Example 2.

The reaction conditions and the evaluation results of the particulatepolyamide of Comparative Example 2 are shown in Table 4.

TABLE 1 Ex. 1 Ex. 2 Ex. 3 Ex. 4 Ex. 5 Ex. 6 Amount of activating 0.030.03 0.03 0.03 0.03 0.03 agent* (molar ratio) Amount of catalyst** 0.010.01 0.01 0.01 0.01 0.01 (molar ratio) Polymerization 40 50 60 40 40 60temperature (° C.) Polymerization 9 20 30 9 9 30 pressure (MPa)Polymerization time 120 120 120 120 120 120 (minutes) Density of 490 780830 490 490 830 compressible fluid (kg/m³) Mixing ratio*** 0.2 0.2 0.20.2 0.2 0.05 Weight average 430,000 370,000 210,000 320,000 270,000260,000 molecular weight (Mw) Particle diameter 53 47 55 51 47 63 (d50)(μm) Particle diameter 2.3 1.9 1.4 2.5 2.4 1.5 dispersion degree Whetherthe polymer Porous Porous Porous Porous Porous Porous is porous.Particle form Spherical Spherical Spherical Spherical SphericalSpherical Maximum value of 0.03 0.01 0.04 0.05 0.06 0.02 (H1/D3)(D1-D2)/D1 0.06 0.02 0.07 0.09 0.11 0.04 Specific surface area 30 43 4928 24 78 (m²/g) Pore diameter peak 61 74 77 63 59 82 ratio (P_(H)/P_(L)) (%) Whether the polymer No No No No No No has shell structure.*The amount of activating agent means a molar ratio of the activatingagent to the monomer (i.e., total amount of 2-pyrrolidone and2-azetidinone). **The amount of catalyst means a molar ratio of thecatalyst to the monomer. ***Mixing ratio means a weight ratio of themonomer to the compressible fluid.

TABLE 2 Ex. 7 Ex. 8 Ex. 9 Ex. 10 Ex. 11 Ex. 12 Amount of activating 0.020.02 0.02 0.02 0.02 0.02 agent (molar ratio) Amount of catalyst 0.010.01 0.006 0.006 0.006 0.003 (molar ratio) Polymerization 40 40 40 40 4040 temperature (° C.) Polymerization 30 20 20 9  9 → 30 20 pressure(MPa) Polymerization time 120 120 120 120 120 120 (minutes) Density of910 840 840 490 490→910 840 compressible fluid (kg/m³) Mixing ratio 0.10.1 0.1 0.1 0.1 0.1 Weight average 19,000 24,000 9,000 13,000 17,0006,000 molecular weight (Mw) Particle diameter 13 22 16 13 10 16 (d50)(μm) Particle diameter 1.3 1.6 1.9 2.9 2.3 2.1 dispersion degree Whetherthe polymer Porous Porous Porous Porous Porous Porous is porous.Particle form Spherical Non- Non- Non- Non- Non- spherical sphericalspherical spherical spherical Maximum value of 0.00 — — — — — (H1/D3)(D1-D2)/D1 0.00 — — — — — Particle form (2)* Circular Slightly ChippedBiconvex Bale Chipped form chipped circular lens form form circularcircular form form form Specific surface area 32 11 16 20 24 18 (m²/g)Pore diameter peak 96 84 81 58 66 74 ratio (P_(H)/P_(L)) (%) Whether thepolymer No No No No No No has shell structure. Adhesiveness Δ ◯ ⊚ ◯ ◯ ⊚*Particle form (2) means the particle form of the particulate polyamidewhen the polyamide is observed from such a direction that the area ofthe projected image is minimal.

TABLE 3 Ex. 1 Ex. 13 Ex. 14 Ex. 15 Ex. 16 Ex. 17 Amount of activating0.03 0.01 0.01 0.005 0.01 0.005 agent (molar ratio) Amount of catalyst0.01 0.015 0.015 0.015 0.015 0.015 (molar ratio) Polymerization 40 50 5060 60 60 temperature (° C.) Polymerization 9 20 30 30 20 20 pressure(MPa) Polymerization time 120 120 120 120 120 120 (minutes) Density of490 780 870 830 720 720 compressible fluid (kg/m³) Mixing ratio 0.2 0.20.2 0.2 0.2 0.2 Weight average 430,000 12,000 10,000 5,000 8,500 6,000molecular weight (Mw) Particle diameter 53 54 26 52 83 54 (d50) (μm)Particle diameter 2.3 1.3 1.5 1.7 1.4 2.1 dispersion degree Whether thepolymer Porous Porous Porous Porous Porous Porous is porous. Particleform Spherical Spherical Spherical Spherical Spherical Spherical Maximumvalue of 0.03 0.06 0.02 0.02 0.05 0.04 (H1/D3) (D1-D2)/D1 0.06 0.11 0.030.04 0.09 0.07 Specific surface area 30 7 10 5 13 2 (m²/g) Pore diameterpeak 61 71 73 94 76 128 ratio (P_(H)/P_(L)) (%) Whether the polymer NoYes Yes Yes Yes Yes has shell structure. Thickness of shell ½ ⅓ ⅕ 1/91/7 1/10 (ratio (t/T)) Gradual emission 5 10 12 20 14 30 controllingability Dissolution rate (1 hr) (%) Dissolution rate (5 hr) (%) 12 22 2430 26 42 Dissolution rate 15 32 36 55 37 60 (10 hr) (%) Dissolution rate18 33 40 70 44 80 (15 hr) (%) Ingredient bearing X ◯ ◯ ⊚ ◯ ⊚ ability

TABLE 4 Comparative Comparative Example 1 Example 2 Amount of activatingagent 0.03 0.03 (molar ratio) Amount of catalyst (molar 0.01 0.01 ratio)Polymerization temperature 40 50 (° C.) Polymerization pressure — 10(MPa) Polymerization time 120 120 (minutes) Density of compressiblefluid — 380 (kg/m³) Mixing ratio — 0.5 Weight average molecular —340,000 weight (Mw) Particle diameter (d50) (μm) — 5 Particle diameterdispersion — 3.6 degree Whether the polymer is Not porous Porous porous.Particle form — Spherical Maximum value of (H1/D3) — 0.03 (D1-D2)/D1 —0.05 Specific surface area (m²/g) — 13 Pore diameter peak ratio — 43(P_(H)/P_(L)) (%) Whether the polymer has No No shell structure.

Effect of this Disclosure

As mentioned above, a particulate polyamide, which includes a polyamide4 and/or a polyamide 3 and which is porous while having a relativelysmall average particle diameter and a narrow particle diameterdistribution can be provided.

This disclosure includes the following embodiments, but is not limitedthereto.

(1) A particulate polyamide which includes at least one of polyamide 4and polyamide 3 and which is porous while having a particle diameter(d50) of from 10 μm to 1,000 μm and a particle diameter dispersiondegree of not greater than 3.0.(2) The particulate polyamide descried in paragraph (1) which ischaracterized by having a substantially spherical form.(3) The particulate polyamide descried in paragraph (1) which ischaracterized by being a non-spherical particulate polyamide which has acircular form when observed from such a direction that the area of theprojected image of the particulate polyamide is maximal while having anon-circular form when observed from such a direction that the area ofthe projected image of the particulate polyamide is minimal.(4) The particulate polyamide descried in paragraph (3) which ischaracterized in that the non-circular form is a form having a recessedportion, a hemispherical form, a polyhedral form, a biconvex lens forms,or a bale form.(5) The particulate polyamide descried in any one of paragraphs (1) to(4) which is characterized by having a specific surface area of not lessthan 10 m²/g.(6) The particulate polyamide descried in any one of paragraphs (1) to(5) which is characterized by having a pore diameter peak ratio(P_(H)/P_(L)) of not less than 0.7, wherein P_(H) represents the heightof a peak in a relatively high diameter range of not less than 100 nm toP_(L) represents the height of a peak in a relatively low diameter rangeof not greater than 50 nm.(7) The particulate polyamide descried in any one of paragraphs (1) to(6) which is characterized by having a shell structure such that ahollow is present in a shell, wherein the ratio of the thickness of theshell to the outer diameter of the particulate polyamide is from 1/10 to⅓.(8) The particulate polyamide descried in paragraph (7) which ischaracterized in that the hollow is communicated with pores in theshell.(9) A method of preparing the particulate polyamide described inparagraph (1) including contacting a base material mixture including amonomer including at least one of 2-pyrrolidone and 2-azetidinone, and abasic polymerization catalyst with a compressible fluid having a densityof not less than 450 kg/m³, and including carbon dioxide to melt ordissolve the base material mixture in the compressible fluid and tosubject the monomer to a ring-opening polymerization reaction.(10) The method described in paragraph (9) which is characterized inthat the density of the compressible fluid is not less than 800 kg/m³.(11) The method described in paragraph (9) or (10) which ischaracterized in that the mixing ratio of the monomer to thecompressible fluid is not greater than 0.3 by weight.(12) The method described in any one of paragraphs (9) to (11) which ischaracterized by further including contacting the ring-openingpolymerization reaction product with a compressible fluid includingcarbon dioxide to remove a reaction residue from the ring-openingpolymerization reaction product.(13) The method described in any one of paragraphs (9) to (11) which ischaracterized by further including contacting the ring-openingpolymerization reaction product with water to remove a reaction residuefrom the ring-opening polymerization reaction product.

Additional modifications and variations of the present invention arepossible in light of the above teachings. It is therefore to beunderstood that within the scope of the appended claims the inventionmay be practiced other than as specifically described herein.

What is claimed is:
 1. A particulate polyamide comprising at least oneof polyamide 4 and polyamide 3, wherein the particulate polyamide isporous and has a particle diameter (d50) of from 10 μm to 1,000 μm and aparticle diameter dispersion degree (Dv/Dn) of not greater than 3.0,wherein Dv represents a volume average particle diameter of theparticulate polyamide and Dn represents a number average particlediameter of the particulate polyamide.
 2. The particulate polyamideaccording to claim 1, wherein the particulate polyamide has asubstantially spherical form.
 3. The particulate polyamide according toclaim 1, wherein the particulate polyamide is a non-sphericalparticulate polyamide which has a circular form when observed from sucha direction that an area of a projected image of the particulatepolyamide is maximal while having a non-circular form when observed fromsuch a direction that the area of the projected image of the particulatepolyamide is minimal.
 4. The particulate polyamide according to claim 3,wherein the non-circular form is a form having a recessed portion, ahemispherical form, a polyhedral form, a biconvex lens forms, or a baleform.
 5. The particulate polyamide according to claim 1, wherein theparticulate polyamide has a specific surface area of not less than 10m²/g.
 6. The particulate polyamide according to claim 1, wherein theparticulate polyamide has a pore diameter peak ratio (P_(H)/P_(L)) ofnot less than 0.7, wherein P_(H) represents a height of a peak in arelatively high diameter range of not less than 100 nm to P_(L)represents a height of a peak in a relatively low diameter range of notgreater than 50 nm.
 7. The particulate polyamide according to claim 1,wherein the particulate polyamide has a shell structure such that ahollow is present in a shell, wherein a ratio of a thickness of theshell to an outer diameter of the particulate polyamide is from 1/10 to⅓.
 8. The particulate polyamide according to claim 7, wherein the hollowis communicated with pores in the shell.
 9. A method of preparing theparticulate polyamide according to claim 1, comprising: contacting abase material mixture, which includes a monomer including at least oneof 2-pyrrolidone and 2-azetidinone, and a basic polymerization catalyst,with a compressible fluid having a density of not less than 450 kg/m³and including carbon dioxide to melt or dissolve the base materialmixture in the compressible fluid and to subject the monomer to aring-opening polymerization reaction.
 10. The method according to claim9, wherein the compressible fluid has a density of not less than 800kg/m³.
 11. The method according to claim 9, wherein a mixing ratio ofthe monomer to the compressible fluid is not greater than 0.3 by weight.12. The method according to claim 9, further comprising: contacting aring-opening polymerization reaction product with a compressible fluidincluding carbon dioxide to remove a reaction residue from thering-opening polymerization reaction product.
 13. The method accordingto claim 9, further comprising: contacting a ring-opening polymerizationreaction product with water to remove a reaction residue from thering-opening polymerization reaction product.